[go: up one dir, main page]

WO2000069538A1 - Procede d'extraction de cuivre a partir d'une solution aqueuse - Google Patents

Procede d'extraction de cuivre a partir d'une solution aqueuse Download PDF

Info

Publication number
WO2000069538A1
WO2000069538A1 PCT/FI2000/000397 FI0000397W WO0069538A1 WO 2000069538 A1 WO2000069538 A1 WO 2000069538A1 FI 0000397 W FI0000397 W FI 0000397W WO 0069538 A1 WO0069538 A1 WO 0069538A1
Authority
WO
WIPO (PCT)
Prior art keywords
extraction
solution
content
viscosity
aqueous solution
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/FI2000/000397
Other languages
English (en)
Inventor
Bror Nyman
Stig-Erik Hultholm
Launo Lilja
Esa Lindell
Eero Ekman
Juhani Lyyra
Raimo Kuusisto
Pertti Pekkala
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Outokumpu Oyj
Original Assignee
Outokumpu Oyj
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Outokumpu Oyj filed Critical Outokumpu Oyj
Priority to BRPI0010471-0A priority Critical patent/BR0010471B1/pt
Priority to US10/019,967 priority patent/US6706186B1/en
Priority to CA002370923A priority patent/CA2370923C/fr
Priority to MXPA01011627A priority patent/MXPA01011627A/es
Priority to AU44079/00A priority patent/AU771155B2/en
Priority to EA200101199A priority patent/EA003234B1/ru
Publication of WO2000069538A1 publication Critical patent/WO2000069538A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D11/04—Solvent extraction of solutions which are liquid
    • B01D11/0446—Juxtaposition of mixers-settlers
    • B01D11/0457—Juxtaposition of mixers-settlers comprising rotating mechanisms, e.g. mixers, mixing pumps
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B15/00—Obtaining copper
    • C22B15/0063—Hydrometallurgy
    • C22B15/0084—Treating solutions
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/26—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • the present invention relates to a method for extracting copper in liquid-liquid solvent extraction from aqueous solutions with a high sulphate content, by raising the viscosity of the extraction solution and by dispersing the aqueous solution into drops, achieving a dense drop aggregation.
  • the viscosity of the extraction solution may be raised either by increasing the content of the actual extractant, the extraction reagent, in the extraction solution or by using a diluting agent with a higher viscosity than that of the diluting agent normally used.
  • By raising the viscosity of the extraction solution the mixing durability of the extraction dispersion can be increased and resulting of that, the amount of residual drops is decreased.
  • Other advantages are that the extraction solution flow of the extraction process decreases in relation to the flow of the aqueous solution acting as the copper source and that the size of the extraction equipment needed is reduced.
  • Dilute aqueous solutions form when poor copper ores are leached directly.
  • the copper content of such solutions is usually of the order of 1 - 4 g/l Cu.
  • neutral salts often accumulate in the solution, mainly aluminium and magnesium sulphates.
  • the sulphate content may rise above 40 g/l, to between 40 and 120 g/l.
  • Some of the sulphate may originate from the ore or the possible use of seawater.
  • the aqueous solution is in a cycle between the extraction and the leaching and thus gradually accumulates the salts which raise the viscosity.
  • Neutral salts can easily cause a viscosity increase harmful to the aqueous solution, even 3 cP, which also disturbs the dispersing of the aqueous and extraction solutions and results in high amounts of residual drops.
  • an increased viscosity in the aqueous solution can make it difficult to achieve such a dispersion.
  • the increased viscosity caused by neutral salts and the resulting disadvantages were not taken into account.
  • the type of extractant is a chelating copper complexing agent, usually hydroxyoxyme, which forms a strong complex with copper, and one fact affecting the progress of copper extraction is how much extractant is present in relation to the amount of copper to be extracted.
  • alifatic or aromatic hydrocarbons kerosenes, with a distillation range between 190 - 245 °C are used as the diluting agent for the copper extractant.
  • the viscosity of these substances is usually below 2 cP, and for aromatics even below 1.5 cP. It is also possible to us mixtures of aromatic and alifatic hydrocarbons as the diluting agent, where the aromatic content of the mixture is around 20 - 30 vol.%.
  • a mixing-durable dispersion means a dispersion where no drops below 0.2 mm appear when the mixing intensity is max. 0.15 kWh/m 3 in a mixing volume of 50 m 3 .
  • Volume-specific mixing power is dependent on the mixing volume so that the power required decreases slightly as the volume increases. Obviously the mixing itself also affects mixing durability.
  • the mixers described in US patent 5,185,081 have been settled on to use in the method according to the present invention. These mixers have a double helix, which helps to avoid locally increasing shear rate forces and the small drops generated as a result.
  • the factor by which the extractant content is raised compared with the normal recommendation in the method according to the present invention varies between 1.2 - 5, and is preferably between 1.5 - 3.
  • the factor may always rise to 5 i.e. according to our invention the extractant content would then be of the order of 7 - 25 vol.%, preferably 15 - 25 vol. %.
  • the preferred extractant content is in the range of 15 - 30 vol.%. Generally, however, the extractant content does not increase above a content of 30% by volume.
  • the viscosity of the extraction solution in this case rises to between 3 - 7 cP, which is enough to raise it to a clearly higher level than the viscosity of the aqueous solution.
  • the aim is to achieve an O/A viscosity ratio of between 1.2 - 3, preferably 1.5 - 2.
  • the extractant content in the extraction solution is presently set in the range of 7 - 30 vol.%, preferably 15 - 30 vol.%.
  • the use of an extractant factor of 1.2 - 2.0 times the recommendation improves the mixing durability of the dispersion.
  • the viscosity of the extraction solution can also be raised partly or wholly with the use of a diluting agent.
  • the distillation range and viscosity of the diluting agents generally used was mentioned earlier as being rather low. If other diluting agents are used, this can also raise the viscosity of the extractant.
  • Alifatic hydrocarbon products can be chosen with a distillation range in the range of 220 - 275 °C or 240 - 270 °C, and the viscosity of these substances measured at a temperature of +25 °C is 2.7 or 3.2 cP. If it is desired to use aromatic hydrocarbons, the viscosity of hydrocarbons with a distillation span of 230 - 290 °C is about 3 cP. It is also possible to use mixtures of alifatic and aromatic hydrocarbons.
  • diluting agent When treating dilute aqueous solutions containing less than 4 g/l of copper, there is a possibility in our invention of using hydrocarbon compounds that boil at a high boiling range as the diluting agent.
  • the use of a diluting agent to increase viscosity is preferred since the diluting agent is always cheaper than the actual extractant.
  • the proportion of diluting agent in the extraction solution can be between 30 - 93%. It is easier to achieve the required rise in viscosity without the density of the extraction solution increasing significantly with alifatic hydrocarbons. The use of alifatic hydrocarbons is also recommended for reasons of industrial hygiene.
  • Figure 1 shows a schematic view of the equipment used in the method of the present invention
  • Figure 3 shows a stage calculation according to the present invention, where the copper content of the PLS is 1.5 g/l and the extractant content of the extraction solution is 15 vol. % Acorga M 5640,
  • Figure 4 shows a stage calculation according to the present invention, where the copper content of the PLS is 1.5 g/l and the extractant content of the extraction solution is 25 vol. % Acorga M 5640,
  • Figure 5 shows a stage calculation according to the prior art, where the copper content of the PLS is 3.0 g/l and the extractant content of the extraction solution is 8.5 vol. % Acorga M 5640,
  • Figure 6 shows a stage calculation according to the present invention, where the copper content of the PLS is 3.0 g/l and the extractant content of the extraction solution is 15 vol. % Acorga M 5640,
  • Figure 7 shows a stage calculation according to the present invention, where the copper content of the PLS is 3.0 g/l and the extractant content of the extraction solution is 25 vol. % Acorga M 5640
  • Figure 8 shows a stage calculation according to the present invention, where the copper content of the PLS is 6.5 g/l and the extractant content of the extraction solution is 22 vol. % Acorga M 5640
  • Figure 9 shows a stage calculation according to the present invention, where the copper content of the PLS is 6.5 g/l and the extractant content of the extraction solution is 30 vol. % Acorga M 5640,
  • Figure 10 shows a stage calculation according to the present invention, where the copper content of the PLS is 6.5 g/l and the extractant content of the extraction solution is 40 vol. % Acorga M 5640
  • Figure 11 shows a stage calculation according to the present invention, where the copper content of the PLS is 2.5 g/l and the extractant content of the extraction solution is 40 vol. % LIX 984N, and
  • Figure 12 shows a stage calculation according to the present invention, where the copper content of the PLS is 32 g/l and the extractant content of the extraction solution is 50 vol. % Acorga M 5640.
  • Figure 1 describes a copper extraction process for treating dilute copper solutions.
  • the process consists of two extraction stages, E1 and E2, one extraction solution washing stage W and one extraction solution stripping stage S. Both the extraction stages and the washing and stripping stages consist of a mixing section 1 , a settler 2, and a pump 3 used to transfer the dispersion.
  • the mixing section has at least one mixer, which is preferably equipped with the mixing devices described earlier.
  • the principles of the extraction stages are the types described in e.g. WO patent application publications 97/40899, 97/40900, 97/40901 and 97/41938.
  • aqueous solution 4 comes first to extraction stage E1 and extraction solution 5 to stage E2.
  • the aqueous solution exiting the final extraction stage E2, raffinate 6, is fed back to ore leaching, and copper-enriched extraction solution 7 is fed from E1 to washing W and stripping S.
  • the extraction solution is circulated via storage tanks.
  • Lean electrolyte 8 is fed from electrolysis to the stripping stage where the copper contained in the organic phase is extracted.
  • the aqueous solution 9 containing copper sulphate exiting the stage goes as rich electrolyte to electrowinning and the stripped organic phase 5 is circulated back to extraction stage E2.
  • Figure 1 shows how considerably the size of the washing and stripping stages of the extraction process is reduced when an extractant is used according to the invention to raise the viscosity of the extraction solution.
  • the reduction is in direct ratio to the external extraction solution pumping, because the mixer-settlers in question are dimensioned directly with the solution flows in all respects, pumping, mixing and solution separation.
  • the mixer and settler volumes of the washing and stripping stages are halved.
  • the actual extraction stages E1 and E2 remain almost their earlier size and the same external extraction solution pumping goes through them, but the extraction solution can be circulated within the stages in order to maintain extraction solution continuity.
  • the extraction solutions flow through each stage of the extraction equipment at essentially the same time.
  • the O/A mixing ratio of the solutions may be reduced according to the method of the invention to below 1 to a value between 0.7 - 1.0, and the size of the extraction stages equipment can be reduced correspondingly.
  • Fig. 1 is only indicative of the relative size of the extraction stages and that of the washing and stripping stages. There are often two stripping stages in an extraction plant and in some cases also two washing stages. Then the savings made by reducing the size of the equipment are correspondingly greater.
  • the amount of extraction solution inside the extraction plant is also reduced correspondingly even if the changes in the amount of extractant itself are not large, since the content of extractant in the extraction solution has been raised. In certain cases it is expedient even to raise the amount of extraction agent circulating in the process, so that the advantages described in the method can be achieved in full measure.
  • the method according to our invention provides the opportunity to treat difficult impurities such as copper ore containing chloride, nitrate or manganese in an economical way.
  • difficult impurities such as copper ore containing chloride, nitrate or manganese
  • ores containing a lot of iron are generally problematic, because iron increases the transfer of the above-mentioned impurities to the electrolyte via the extraction solution. This results in a situation where it is even more important than before to prevent the transfer of said impurities first to the extraction solution with the unseparated drops of aqueous solution from extraction stage E1 to washing stage W and from there on to stripping stage S.
  • the result is an aqueous solution with a copper content in the range of 1 - 4 g/l, and in addition neutral salts accumulate in the solution.
  • the sulphate content of the solution may rise to between 40 - 120 g/l, which causes a rise in the viscosity of the aqueous solution, but on the other hand, sulphate has the benefit of acting as a pH buffer when using copper extraction in the pH range of 0.8 - 2.2. In other words it improves the equilibrium of the copper extraction and makes more copper transfer to the extraction solution.
  • the aqueous solution was made using ion-exchanged water, copper sulphate and sulphuric acid.
  • the copper content of the solution was 2 g/l, the sulphate content 52 g/l and the pH 1.8.
  • the extraction solution was prepared by mixing the commercial extractants shown in the table in different proportions with a commercial kerosene solution D70 as diluting agent. Mixing contact was made between the extraction solutions and the copper sulphate solution (aqueous solution) at room temperature and in the O/A phase ratio of 1.0, thereby obtaining the copper content values of the solutions in the table. After mixing all the solutions were recovered and stored for two weeks before the actual mixing tests. This ensured that the extraction solutions in particular corresponded to the solutions used in normal extraction, without the drawbacks of new extraction solutions.
  • a double helix agitator as described in US patent 5,185,081 with a diameter of 152 mm and height of 174 mm was used in the mixing tests.
  • the mixer itself was a flat-bottomed cylinder with a diameter of 214 mm and effective solution depth also of 214 mm.
  • the cylinder was equipped with four baffles positioned on the frame of the cylinder, with a width of 18 mm and at a distance of 3.5 mm from the inner surface of the cylinder.
  • the mixing contact itself was made at room temperature and in the O/A phase ratio of 1.0 so that the extraction solution was continuous in all tests and the aqueous solution in drops.
  • the revolution speed of the mixer was 220 rpm and the duration of mixing was 3 minutes in all tests.
  • each extraction solution was mixed with a new batch of the aqueous solution. After mixing the solutions were made to separate by the effect of gravity. 15 minutes after mixing the amount of residue solution in each of the separated solutions was determined.
  • the drop residues (entrainment levels) are shown in Table 1 , where A/O means water in the extraction solution and O/A means organic phase drops in the aqueous solution.
  • aqueous solution was prepared with a copper content of 1.5 g/l, sulphate content of 50 g/l and pH of 1.8.
  • Three different extraction solutions were also prepared: 1. Acorga M5640 5.0 vol.-%
  • the first solution represents an extraction solution according to the prior art.
  • Extraction equilibrium curves EEQ and stripping equilibrium curves SEQ shown in Figs 2, 3 and 4 were defined for the extraction solutions and aqueous solutions in question with the method used by experts in this field.
  • Diagram 2 shows the prior art, diagrams 3 and 4 the method according to this invention.
  • an extraction calculation was made for a copper extraction process with two extraction stages functioning on the counterflow principle and two stripping stages. The calculation was made on the basis of the McCabe-Thiele method, familiar to specialists in the field.
  • the extraction and stripping stages reach as far as the equilibrium curve, because the stage efficiency is very high when using for instance the equipment described in WO patent publications.
  • the three stage calculations presented in the example show that the copper extraction yield remains at a good level and almost unchanged, even though the external pumping of the extraction solution is reduced.
  • the copper contents of the raffinate are in all cases 0.2 - 0.4 g/l.
  • the lowest content is obtained by raising the extractant content to 15%, whereby the external pumping of the extraction solution can be reduced to 35% of the PLS (pregnant leach solution) feed i.e. copper-containing aqueous solution feed.
  • stripping equilibrium allows the making of strong copper electrolyte when the copper content of the extraction solution can be lowered sufficiently. This means the level where the extraction equilibrium is still rising sharply in an aqueous solution Cu content of under 0.5 g/l, as stated earlier.
  • stage calculation reveals that with the method according to the present invention, a significant improvement is achieved in the copper content of the electrolyte going to copper electrolysis. With two stripping stages the electrolyte was made almost saturated as regards copper sulphate.
  • the extraction solution In stripping stage S1 the extraction solution on the other hand falls from an LO (loaded organic) value of 6.7 g/l to 4.2 as the Cu content of the copper electrolyte rises from 40.4 g/l to 50.0 g/l.
  • the Cu content of the extraction solution falls further to a BO (barren organic) value of 3.0 in stripping stage S2, from where the extraction solution moves on to extraction stage E2 of the extraction.
  • stage calculations The important points in said stage calculations are the so-called operating lines which indicate the contents in which the solutions touch each other when entering or leaving the first extraction and stripping stages E1 and S1 and the final extraction and stripping stages E2 and S2 and in between said stages. From the nature of the stage calculations it follows that the gradient of the operating lines indicate the external solution pumping i.e. the ratio of PLS and extraction solution flows in extraction as well as the ratio of electrolyte and extraction solution flows in stripping. It has been possible to calculate from the external pumping ratios how much the electrolyte circulation is reduced with our method in relation to the amount of PLS flow.
  • an aqueous solution was used with a Cu content of 6.5 g/l, in other words richer than is usually achieved with direct leaching of any poor ore.
  • our method has distinct advantages.
  • the stage calculations of diagrams 8, 9 and 10 were used.
  • the contents of the extraction solution are 22, 30 and 40 vol.%, the extractant Acorga M6540 and the diluting agent again kerosene D70.
  • the temperature of the extraction solution was 18 °C.
  • the external pumping of the electrolyte in ratio to the external pumping of the PLS also settles at the same value of 0.15.
  • the extractant used was the commercial chemical LIX 984N, which is similar to the reagent used in the previous example, and again kerosene D70 was the diluting agent.
  • the extractant content was 50 vol.%. Table 5
  • the example shows how high the copper content of the PLS can be raised using our invention.
  • the Cu content of the PLS was raised up to 32 g/l while the extractant content of the extraction solution was raised to 50 vol.%, with Acorga M5640 as reagent and kerosene D70 as diluting agent.
  • Mixing with the double helix mixer mentioned above is successful, even though an extractant content of as much as 40 - 70 vol.% is used. It is advantageous to do this when it is desired to reduce external pumping of the extraction solution.
  • the stage calculation concerning 50 vol.% in Fig.12 and the summary in Table 6 clarify these possibilities further. Table 6

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Mechanical Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Geology (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Extraction Or Liquid Replacement (AREA)
  • Electrolytic Production Of Metals (AREA)

Abstract

L'invention concerne un procédé d'extraction de cuivre dans une extraction liquide-liquide par solvant, à partir d'une solution aqueuse comprenant une teneur élevée en sulfate, ce procédé consistant à élever la viscosité de la solution d'extraction et à disperser la solution aqueuse en gouttelettes, de manière à obtenir une agglomération dense des gouttelettes. On peut élever la viscosité de la solution d'extraction soit en augmentant, dans la solution d'extraction, la teneur de l'agent extractant utilisé, du réactif d'extraction, soit en utilisant un agent de dilution possédant une viscosité supérieure à celle de l'agent de dilution généralement utilisé. En élevant la viscosité de la solution d'extraction, on peut augmenter la durabilité du mélange de la dispersion d'extraction, ce qui contribue à faire diminuer la quantité de gouttelettes résiduelles. D'autres avantages résident en ce que l'écoulement de la solution d'extraction du procédé d'extraction décroît par rapport à l'écoulement de la solution aqueuse agissant en tant que source de cuivre, et en ce que la dimension du matériel d'extraction requis est réduite.
PCT/FI2000/000397 1999-05-14 2000-05-04 Procede d'extraction de cuivre a partir d'une solution aqueuse Ceased WO2000069538A1 (fr)

Priority Applications (6)

Application Number Priority Date Filing Date Title
BRPI0010471-0A BR0010471B1 (pt) 1999-05-14 2000-05-04 método para extração lìquido-lìquido de cobre de uma solução aquosa.
US10/019,967 US6706186B1 (en) 1999-05-14 2000-05-04 Method for extracting copper from an aqueous solution
CA002370923A CA2370923C (fr) 1999-05-14 2000-05-04 Procede d'extraction de cuivre a partir d'une solution aqueuse
MXPA01011627A MXPA01011627A (es) 1999-05-14 2000-05-04 Un metodo para extraer cobre de una solucion acuosa.
AU44079/00A AU771155B2 (en) 1999-05-14 2000-05-04 A method for extracting copper from an aqueous solution
EA200101199A EA003234B1 (ru) 1999-05-14 2000-05-04 Способ извлечения меди из водного раствора

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FI991111A FI105829B (fi) 1999-05-14 1999-05-14 Menetelmä kuparin uuttamiseksi vesiliuoksista
FI991111 1999-05-14

Publications (1)

Publication Number Publication Date
WO2000069538A1 true WO2000069538A1 (fr) 2000-11-23

Family

ID=8554671

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/FI2000/000397 Ceased WO2000069538A1 (fr) 1999-05-14 2000-05-04 Procede d'extraction de cuivre a partir d'une solution aqueuse

Country Status (12)

Country Link
US (1) US6706186B1 (fr)
CN (1) CN1142004C (fr)
AR (1) AR023946A1 (fr)
AU (1) AU771155B2 (fr)
BR (1) BR0010471B1 (fr)
CA (1) CA2370923C (fr)
EA (1) EA003234B1 (fr)
FI (1) FI105829B (fr)
MX (1) MXPA01011627A (fr)
PE (1) PE20010256A1 (fr)
WO (1) WO2000069538A1 (fr)
ZA (1) ZA200108935B (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2002092863A1 (fr) * 2001-05-11 2002-11-21 Outokumpu Oyj Procede d'extraction

Families Citing this family (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20060112067A1 (en) * 2004-11-24 2006-05-25 Morris Robert P Interactive system for collecting metadata
RU2336346C1 (ru) * 2007-04-16 2008-10-20 Государственное образовательное учреждение высшего профессионального образования "Московский государственный институт стали и сплавов" (технологический университет) Способ извлечения металлов из сульфатных растворов, содержащих железо
CN101435022B (zh) * 2007-11-13 2011-09-07 北京有色金属研究总院 一种控制硫化铜矿生物浸出液萃取过程中第三相形成的工艺
JP4717908B2 (ja) * 2008-08-11 2011-07-06 Ｊｘ日鉱日石金属株式会社 銅を含有する塩化物浴からの銅の回収方法
FI121470B (fi) * 2009-03-27 2010-11-30 Outotec Oyj Laitteisto ja menetelmä kuparia sisältävän orgaanisen uuttoliuoksen puhdistamiseksi epäpuhtauksista
JP6046612B2 (ja) 2010-07-02 2016-12-21 エクソンモービル アップストリーム リサーチ カンパニー 低エミッショントリプルサイクル発電システム及び方法
CN102181636B (zh) * 2011-05-17 2012-11-28 重庆海祥医药化工有限公司 一种改性β-二酮萃取剂
CN103173616A (zh) * 2011-12-23 2013-06-26 北京石油化工学院 微乳液萃取分离废弃锂离子电池浸出液中铜和钴的方法
CN117225004B (zh) * 2023-11-14 2024-01-26 湖南禧又多油脂有限公司 一种基于物联网的植物油低温萃取处理自动控制系统

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4221658A (en) * 1977-02-21 1980-09-09 Davy International (Oil & Chemicals) Limited Effecting liquid-liquid contact
GB2117666A (en) * 1982-03-09 1983-10-19 Univ Manchester Emulsification
US5185081A (en) * 1990-04-04 1993-02-09 Outokumpu Oy Method and apparatus for mixing and separating two liquid phases while preventing aeration and emulsions using a mixer-settler
US5662871A (en) * 1993-12-02 1997-09-02 Outokumpu Engineering Contractors Oy Method for extracting metals from large solution flows and apparatus for realizing the same

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3666446A (en) * 1969-11-12 1972-05-30 Pyrites Co Inc The Process for solvent extraction of metals
US4173616A (en) * 1978-03-07 1979-11-06 Shell Oil Company Extraction of copper values from aqueous solution
DE3876941D1 (de) * 1987-10-28 1993-02-04 Solvay Umweltchemie Gmbh Zur selektiven abtrennung von metallkationen aus waessrigen loesungen geeignetes teilchenfoermiges mittel, verfahren zu seiner herstellung und seine verwendung.
US5273654A (en) * 1992-06-08 1993-12-28 Aquatechnology Resource Management Solvent removal system
US6242625B1 (en) * 1999-09-30 2001-06-05 Henkel Corporation Process for extracting copper values from copper containing ores

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4221658A (en) * 1977-02-21 1980-09-09 Davy International (Oil & Chemicals) Limited Effecting liquid-liquid contact
GB2117666A (en) * 1982-03-09 1983-10-19 Univ Manchester Emulsification
US5185081A (en) * 1990-04-04 1993-02-09 Outokumpu Oy Method and apparatus for mixing and separating two liquid phases while preventing aeration and emulsions using a mixer-settler
US5662871A (en) * 1993-12-02 1997-09-02 Outokumpu Engineering Contractors Oy Method for extracting metals from large solution flows and apparatus for realizing the same

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2002092863A1 (fr) * 2001-05-11 2002-11-21 Outokumpu Oyj Procede d'extraction
US7390468B2 (en) 2001-05-11 2008-06-24 Outotec Oyj Extraction process

Also Published As

Publication number Publication date
AU771155B2 (en) 2004-03-18
FI991111A0 (fi) 1999-05-14
AR023946A1 (es) 2002-09-04
BR0010471B1 (pt) 2011-12-13
MXPA01011627A (es) 2002-06-04
AU4407900A (en) 2000-12-05
BR0010471A (pt) 2002-02-13
CN1350473A (zh) 2002-05-22
PE20010256A1 (es) 2001-03-21
EA200101199A1 (ru) 2002-04-25
US6706186B1 (en) 2004-03-16
CA2370923A1 (fr) 2000-11-23
EA003234B1 (ru) 2003-02-27
FI105829B (fi) 2000-10-13
ZA200108935B (en) 2002-09-10
CA2370923C (fr) 2008-07-29
CN1142004C (zh) 2004-03-17

Similar Documents

Publication Publication Date Title
US5670035A (en) Method for recovering copper
US5849172A (en) Copper solvent extraction and electrowinning process
CA2699893C (fr) Circuit de recuperation de cuivre par lixiviation controlee
US6706186B1 (en) Method for extracting copper from an aqueous solution
US4039405A (en) Leaching copper ores and solvent extraction of the copper-bearing solutions
EP0786021B1 (fr) Procede pour fabriquer des feuilles de cuivre
CA1119817A (fr) Methode de separation du cuivre metallique
US6350354B1 (en) Modular solvent extraction plant
CA1073368A (fr) Procede de separation de phases dans un melange a trois phases
US4551314A (en) Process for improving solvent extraction operation using two mixers
EP2411549B1 (fr) Appareil et procédé d'élimination d'impuretés dans le cadre d'une extraction liquide/liquide de cuivre
JPH0776391B2 (ja) 亜鉛回収法
DE2203222A1 (de) Verfahren zum Herstellen metallischen Kupfers
CN105624403B (zh) 一种废酸的综合利用方法
US4421616A (en) Method of producing zinc from chloride solutions which contain chiefly iron, copper and zinc
AU2007280103B2 (en) Process for improving phase separations in solvent extraction circuits of metal winning
Pandey et al. Extraction of nickel and copper from the ammoniacal leach solution of sea nodules by LIX 64N
Prasad et al. Development of SX-EW process for copper recovery—an overview
RU2336346C1 (ru) Способ извлечения металлов из сульфатных растворов, содержащих железо
Spence et al. Practical aspects of copper solvent extraction from acidic leach liquors
NO157742B (no) FremgangsmŸte ved utvinning av metaller i metallsulfidholdige materialer.
Molnar Solvent Extraction
US1342804A (en) Metallurgical process
RU2339714C1 (ru) Способ экстракции меди из сернокислых растворов, содержащих ионы двухвалентного железа
AU728933B2 (en) Method for recovering copper

Legal Events

Date Code Title Description
WWE Wipo information: entry into national phase

Ref document number: 00807555.7

Country of ref document: CN

AK Designated states

Kind code of ref document: A1

Designated state(s): AE AL AM AT AU AZ BA BB BG BR BY CA CH CN CU CZ DE DK EE ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MD MG MK MN MW MX NO NZ PL PT RO RU SD SE SG SI SK SL TJ TM TR TT UA UG US UZ VN YU ZA ZW

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): AM AZ BY KG KZ MD RU TJ TM AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE

121 Ep: the epo has been informed by wipo that ep was designated in this application
DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
WWE Wipo information: entry into national phase

Ref document number: 2001/08935

Country of ref document: ZA

Ref document number: 200108935

Country of ref document: ZA

WWE Wipo information: entry into national phase

Ref document number: IN/PCT/2001/01380/MU

Country of ref document: IN

ENP Entry into the national phase

Ref document number: 2370923

Country of ref document: CA

Ref document number: 2370923

Country of ref document: CA

Kind code of ref document: A

WWE Wipo information: entry into national phase

Ref document number: PA/a/2001/011627

Country of ref document: MX

WWE Wipo information: entry into national phase

Ref document number: 200101199

Country of ref document: EA

REG Reference to national code

Ref country code: DE

Ref legal event code: 8642

WWE Wipo information: entry into national phase

Ref document number: 10019967

Country of ref document: US

122 Ep: pct application non-entry in european phase
NENP Non-entry into the national phase

Ref country code: JP